JPS6023109B2 - Carbamate condensation method in urea synthesis equipment - Google Patents
Carbamate condensation method in urea synthesis equipmentInfo
- Publication number
- JPS6023109B2 JPS6023109B2 JP51045614A JP4561476A JPS6023109B2 JP S6023109 B2 JPS6023109 B2 JP S6023109B2 JP 51045614 A JP51045614 A JP 51045614A JP 4561476 A JP4561476 A JP 4561476A JP S6023109 B2 JPS6023109 B2 JP S6023109B2
- Authority
- JP
- Japan
- Prior art keywords
- carbamate
- condenser
- tube bundle
- condensing
- head
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C273/00—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups
- C07C273/02—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds
- C07C273/04—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds from carbon dioxide and ammonia
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
【発明の詳細な説明】
本発明は尿素合成においてカルバミン酸塩を凝縮する方
法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for condensing carbamates in urea synthesis.
尿素合成の各種の方法において、カルバミン酸塩の数段
階の分解より生成したＮＨ３、Ｃ抄および均○の混合蒸
気を凝縮するためおよびカルバミン酸塩を反応器に再循
環するため普通熱交換器が設られている。In various methods of urea synthesis, a heat exchanger is commonly used to condense the mixed vapor of NH3, C-cut, and homogenate produced from the several-step decomposition of carbamate and to recycle the carbamate to the reactor. It is set up.
ストリツピング操作では、ほとんどすべてのカルバミン
酸塩は反応器の圧力と実質的に同等の圧力で単一操作で
再循環できる。In a stripping operation, nearly all of the carbamate can be recycled in a single operation at a pressure substantially equivalent to that of the reactor.
また反応器と実質的に同等の圧力で操作される蒸留器（
ストリッパー）で得られるＮＨ３、Ｃｏ２および＆○の
混合蒸気は高温度でカルバミン酸塩凝縮器で凝縮する。
上記凝縮により発生した熱は水蒸気の発生のため高い熱
しベルで除去される。普通の方法では、カルバミン酸塩
は順次減少する圧力下で操作する数個の工程に再循環さ
れる。Also, a distiller operated at substantially the same pressure as the reactor (
The mixed vapor of NH3, Co2 and &○ obtained in the stripper) is condensed at high temperature in a carbamate condenser.
The heat generated by the condensation is removed in a high heating bell for the generation of water vapor. In a common process, the carbamate is recycled to several steps operating under successively decreasing pressures.
これらの操作圧力は合成反応器の圧力から実質的に相異
している。カルバミン酸塩の凝縮熱の１部分のみがカル
バミン酸塩凝縮器で水蒸気を発生するに十分に高いレベ
ルで回収されるにすぎない。カルバミン酸塩凝縮器はよ
り高圧下で操作される。すべての場合、Ｎ比、Ｃｏ２、
および日２０の混合蒸気の凝縮はより高圧下で操作する
カルバミン酸塩の再循還の段階で遭遇するような水含量
の少ないＮＨ３、Ｃｏ２および比０の混合蒸気組成の場
合には重要な操作である。These operating pressures differ substantially from the synthesis reactor pressure. Only a portion of the heat of condensation of the carbamate is recovered at a level high enough to generate water vapor in the carbamate condenser. Carbamate condensers operate under higher pressure. In all cases, N ratio, Co2,
The condensation of the mixed steam at 20 and 20 days is an important operation in the case of mixed steam compositions with low water content of NH3, Co2 and ratio 0, such as encountered in the carbamate recirculation stage, which operates under higher pressures. It is.
凝縮するＮＨ３、Ｃｏ２および日２０の混合蒸気が特に
高圧蒸留工程から来る場合、この場合水舎量は少ない。If the condensing mixed vapor of NH3, Co2 and 20% comes from a high pressure distillation process, in this case the amount of water is small.
凝縮を可能にするためには、カルバミン酸塩凝縮液は蒸
気と共にまたより低圧で操作するカルバミン酸塩の凝縮
および再循環工程で普通に得られる水にとんだ炭酸塩溶
液と共に凝縮器に供給される。この場合高圧は１００な
し、し３０ぴ気圧、低圧は２ないし５悦気圧である。上
記溶液は吸収剤であり、ＮＨ３、Ｃ０２および比○の混
合蒸気と添加溶液との間で均一な分散がなされることが
非常に重要である。To enable condensation, the carbamate condensate is fed to the condenser together with steam and with the aqueous carbonate solution normally obtained in carbamate condensation and recirculation processes operating at lower pressures. . In this case, the high pressure is between 100 and 30 pressures, and the low pressure is between 2 and 5 pressures. The above solution is an absorbent, and it is very important that there is a uniform dispersion between the mixed vapor of NH3, CO2 and ratio O and the additive solution.
この結果は蒸気と添加する炭酸塩とを混合および分散す
る適当な装置を用いて普通の技術でなされる。This result is accomplished by conventional techniques using suitable equipment for mixing and dispersing the steam and added carbonate.
公知の技術では、蒸気と吸収液とを均一に分散するため
、より高圧で操作するカルバミン酸塩凝縮器は一般に管
内部の処理流体に対して堅型である。In the known art, carbamate condensers operating at higher pressures are generally rigid with respect to the process fluid inside the tube in order to uniformly distribute the vapor and absorbent liquid.
凝縮は第１図の凝縮器で実施される。ＮＨ３、Ｃ０２お
よび日２０の混合蒸気は導管３から供給され、混合器４
において導管２によって低圧工程からくる炭酸アンモニ
ウム溶液と混合される。混合物は導管５から堅型凝縮器
１に供給される。該凝縮器は導管６から供給され循環す
る水のジャケットを備えている。発生した水蒸気は導管
９を通って凝縮器１のジャケットから流出して水蒸気分
離器７に送られこ）から水６および発生した水蒸気８が
得られる。得られたカルバミン酸アンモニウムの溶液は
導管１０から取出される。Condensation is carried out in the condenser of FIG. A mixed vapor of NH3, C02 and NH20 is supplied from conduit 3 and mixer 4
In the conduit 2 it is mixed with the ammonium carbonate solution coming from the low pressure step. The mixture is fed through conduit 5 to vertical condenser 1 . The condenser is equipped with a jacket of circulating water supplied by conduit 6. The generated steam leaves the jacket of the condenser 1 through conduit 9 and is sent to a steam separator 7) from which water 6 and generated steam 8 are obtained. The resulting ammonium carbamate solution is removed via conduit 10.
熱が水蒸気の発生によって除かれる場合、適当にカルバ
ミン酸塩凝縮器に連結されている生成水蒸気の分離装置
が設けられている。If the heat is removed by the generation of steam, a separation device for the produced steam, suitably connected to the carbamate condenser, is provided.
凝縮器を正しく操作する目的および最高の水準でＮＨ３
、Ｃ０２および日２０の混合蒸気を凝縮するときに発生
する熱を回収するためには、熱交換器の入口に非常に高
価な分配装置を設けるのが普通である。NH3 for the purpose of correct operation of the condenser and the highest standards
In order to recover the heat generated when condensing the mixed steam of , C02 and 20, it is common to provide a very expensive distribution device at the inlet of the heat exchanger.
上記分配装置を正確に操作することおよび偏流を防止す
ることは厄介な問題である。Correct operation of the distribution device and prevention of drift are problematic.
その理由はカルバ‐ミン酸塩の結晶化のため姿閉現象が
起こるためである。加えるに、支持構造のため堅型の熱
交換器を設けることは非常に費用がか）る。The reason is that a figure-closing phenomenon occurs due to the crystallization of carbamate. In addition, it is very expensive to provide a rigid heat exchanger because of the support structure.
特に大童生産の設備を設ける場合にはなお更である。ま
た分離器は熱除去で発生した水蒸気のためにも設ける必
要がある。更に装置がかなり大型の場合（高容量の装置
）には均一分散を達成することは非常に困難である。本
発明は、低圧工程から来る炭酸アンモニウム塩の溶液よ
り成りしかも高圧（５０なし、し３００気圧）における
カルバミン酸塩のの分解から来る。This is especially true when installing Odo production equipment. A separator must also be provided for the water vapor generated during heat removal. Furthermore, it is very difficult to achieve uniform dispersion if the equipment is quite large (high capacity equipment). The invention consists of a solution of ammonium carbonate salts coming from a low pressure process and from the decomposition of carbamates at high pressures (50 to 300 atmospheres).
Ｎ馬、Ｃ０２および日２０の混合蒸気によって構成され
る混合物が静“頭圧”△Ｐに維持された５０ないし３０
疎気圧の入口圧で水平の管型凝縮城に導入されるならば
上記すべての欠点は容易に除去することができることを
発見したことは驚くべきことである。△Ｐの値は０．５
ないし５気圧の範囲であるしかもこの値は従来公知のい
ずれの装置についても得ることができる。A mixture composed of a mixed vapor of N, C02 and 20 days was maintained at a static "head pressure" △P of 50 to 30
It was surprising to discover that all the above-mentioned drawbacks can be easily eliminated if introduced into a horizontal tube-type condensing castle with an aphobic inlet pressure. The value of △P is 0.5
to 5 atmospheres, and this value can be obtained with any conventionally known device.
これらのうちで減少した値、好ましくは出口における液
頭はＡＨである。本発明方法は水平管東と出口において
一定の液頭とを有する凝縮器で実施するのが有利である
。The reduced value of these, preferably the liquid head at the outlet, is AH. The process according to the invention is advantageously carried out in a condenser with a horizontal pipe and a constant liquid head at the outlet.
水平管の管束の最も外側をとりまく円周蚤Ｄに対する液
頭△日の比は５なし、し３０、好ましくは１０であるも
のが有利である。２０％以上の液を含む蒸気が凝縮器に
入って凝縮し、凝縮器から溶液が排出される。Advantageously, the ratio of the liquid head Δ to the circumferential flea D surrounding the outermost tube bundle of horizontal tubes is between 5 and 30, preferably 10. The vapor containing more than 20% liquid enters the condenser and condenses, and the solution is discharged from the condenser.
一方凝縮熱はうばわれ凝縮器のジャケット内で水蒸気が
発生する。本発明を第２図によって説明するがこれに限
定されない。On the other hand, the heat of condensation is lost and water vapor is generated within the jacket of the condenser. The present invention will be explained with reference to FIG. 2, but is not limited thereto.
水平管型凝縮器１には低圧分解工程から釆る炭酸塩溶液
２がカルバミン酸塩の高圧分解によって得られる混合ガ
ス３と共に送られる。A carbonate solution 2 from the low-pressure decomposition process is sent to the horizontal tube condenser 1 together with a gas mixture 3 obtained by high-pressure decomposition of carbamates.
水平型蒸発器には排出用管５が設けられておりのぞむ液
頭△日６に維持される。この液頭は炭酸塩とＮＨ３、Ｃ
０２および日２０の凝縮液との混合物に打勝ち、このと
き発生した水蒸気は管４により蒸発器１から出る。本発
明方法の利点は次の如くである。The horizontal evaporator is provided with a discharge pipe 5 to maintain the desired liquid head. This liquid head consists of carbonate, NH3, C
The water vapor thus generated leaves the evaporator 1 via pipe 4, overcoming the mixture with the condensate of 02 and 20 days. The advantages of the method of the present invention are as follows.
【１｝ 投下資本を軽減できること。[1] Invested capital can be reduced.
すなわち蒸気の発生によって熱が除去されるとき分配装
置を省略できること、支持用構造体が省略できること、
および水蒸気分離器が省略できることである。【２｝
カルバミン酸塩の析出または偏流を作らないで最適条件
で安定した操作ができることである。i.e., when heat is removed by steam generation, distribution devices can be omitted, supporting structures can be omitted,
and the steam separator can be omitted. [2}
Stable operation can be performed under optimal conditions without carbamate precipitation or drift.
糊 凝縮が高圧下で起こるため高能率で熱の除去ができ
ること。Glue Since condensation occurs under high pressure, heat can be removed with high efficiency.
すなわち良品質の水蒸気が発生することである。次に実
施例を掲げて本発明を説明する。In other words, high quality water vapor is generated. Next, the present invention will be explained with reference to Examples.
例
第２図に示す湯沸し型、すなわち水平管東型熱交換器１
について本発明を説明する。Example Water boiler type shown in Figure 2, that is, horizontal pipe east type heat exchanger 1
The present invention will be explained with respect to the following.
カルバミン酸塩分解域（図示せず）から釆る１５唯気圧
の蒸気３（温度１９０００、流速６０トン）が低圧城か
ら再循環ししかも前以て１５０気圧（溶液温度７０こ○
、流速２５トン）に昇圧して炭酸アンモニウムの水溶液
２と混合した後管東の管７の内部で凝縮される。Steam 3 (temperature 19,000, flow rate 60 tons) at a pressure of 15 mA (temperature 19,000 mA, flow rate 60 tons) emanating from the carbamate decomposition zone (not shown) is recirculated from the low-pressure castle and pre-heated at 150 atm (temperature 70 mA).
, a flow rate of 25 tons) and mixed with the aqueous solution 2 of ammonium carbonate, and then condensed inside the tube 7 on the east side of the tube.
熱はジャケット側で液相を沸騰することによって除かれ
る。Heat is removed by boiling the liquid phase on the jacket side.
その結果水蒸気４が作られる。△Ｈ／Ｄの比は１酪維持
され、かかる条件下では水平管東凝縮器の管は完全に液
体で満たされ凝縮は妨害されることなく行なわれる。発
生した水蒸気は１４７０の温度である。As a result, water vapor 4 is produced. The ratio of ΔH/D is maintained at 1, and under such conditions the tubes of the horizontal tube east condenser are completely filled with liquid and condensation occurs unhindered. The generated water vapor has a temperature of 1470°C.
一方従来の装置では１斑。０以上の温度の水蒸気を発生
させることはできない。On the other hand, with the conventional device, there is only one spot. It is not possible to generate water vapor at a temperature higher than 0.
第１図は従来の堅型凝縮器の系統図、第２図は本発明の
水平管東型凝縮器の系統図を示す。
１・…・・堅型凝縮器、２，３，５，６．９・・・・・
・導管、４・…・・混合器、７・・・・・・水蒸気分離
器、８・・・・・・発生水蒸気、１０・・・・・・出口
管。
Ｆｉ ．Ｉ
Ｆｉ．２FIG. 1 shows a system diagram of a conventional vertical condenser, and FIG. 2 shows a system diagram of a horizontal pipe east type condenser of the present invention. 1...Right condenser, 2, 3, 5, 6.9...
- Conduit, 4...Mixer, 7... Steam separator, 8... Generated steam, 10... Outlet pipe. Fi. I Fi. 2
Claims (1)
程でカルバミン酸塩の分解によって得られるＮＨ＿３、
Ｃｏ＿２およびはＨ＿２Ｏの蒸気との混合物を凝縮域に
供給する工程を含む尿素合成装置においてカルバミン酸
塩を凝縮する方法において、凝縮域は静頭（Δｐ）を有
する水平管束凝縮器でしかも該凝縮器は０．５ないし５
気圧の静頭に維持されることを特徴とする尿素合成装置
におけるカルバミン酸塩の凝縮方法。 ２ 水平管束凝縮器は出口においてＮＨ＿３、Ｃｏ＿２
およびＨ＿２Ｏの凝縮蒸気と炭酸塩溶液との混合物に打
勝つ液頭（ΔＨ）を有する水平管束凝縮器である特許請
求の範囲第１項記載の方法。 ３ 水平管の管束の最も外側管をとりまく円周径（Ｄ）
に対する液頭（ΔＨ）の比は５ないし３０、好ましくは
１０である前記第２項記載の方法。 ４ 管束に入る混合物中の液体含量は２０％以上である
前記第２項および第３項のいずれかに記載の方法。 ５ 凝縮は水蒸気の発生と同時に行なわれる特許請求の
範囲および前記各項のいずれかに記載の方法。[Claims] 1. NH_3 obtained by decomposition of the ammonium carbonate salt solution coming from the low-pressure step and the carbamate in the high-pressure step,
A method for condensing carbamate in a urea synthesizer comprising supplying a mixture of Co_2 and H_2O vapors to a condensing zone, the condensing zone being a horizontal tube bundle condenser with a static head (Δp) and the condensing zone being a horizontal tube bundle condenser having a static head (Δp); is 0.5 to 5
A method for condensing carbamate in a urea synthesis apparatus, characterized in that the atmospheric pressure is maintained at a static head. 2 The horizontal tube bundle condenser has NH_3, Co_2 at the outlet.
2. The method of claim 1, wherein the condenser is a horizontal tube bundle condenser having a liquid head (ΔH) that overcomes the mixture of condensed vapor of H_2O and carbonate solution. 3 Circumference diameter (D) surrounding the outermost pipe of the horizontal pipe bundle
3. The method according to claim 2, wherein the ratio of the liquid head (ΔH) to the liquid head is between 5 and 30, preferably 10. 4. The method according to any one of the above items 2 and 3, wherein the liquid content in the mixture entering the tube bundle is 20% or more. 5. The method according to any of the claims and the preceding clauses, wherein the condensation is carried out simultaneously with the generation of water vapor.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| IT2261575A IT1037576B (en) | 1975-04-23 | 1975-04-23 | Ammonium carbonate condensation in urea synthesis - by contacting liq. and vapour phases in a horizontal heat exchanger (NL261076) |
| IT22615A/75 | 1975-04-23 | ||
| AU15623/76A AU506832B2 (en) | 1975-04-23 | 1976-07-06 | Formation of ammonium carbamate solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS51128917A JPS51128917A (en) | 1976-11-10 |
| JPS6023109B2 true JPS6023109B2 (en) | 1985-06-05 |
Family
ID=25616093
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP51045614A Expired JPS6023109B2 (en) | 1975-04-23 | 1976-04-23 | Carbamate condensation method in urea synthesis equipment |
Country Status (14)
| Country | Link |
|---|---|
| US (1) | US4082797A (en) |
| JP (1) | JPS6023109B2 (en) |
| AT (1) | AT344197B (en) |
| AU (1) | AU506832B2 (en) |
| BE (1) | BE844047A (en) |
| CA (1) | CA1069932A (en) |
| CH (1) | CH622006A5 (en) |
| CS (1) | CS196306B2 (en) |
| DE (1) | DE2617185C3 (en) |
| FR (1) | FR2308615A1 (en) |
| GB (1) | GB1506129A (en) |
| IN (1) | IN144536B (en) |
| NL (1) | NL167157C (en) |
| SE (1) | SE423386B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IT1068268B (en) * | 1976-09-09 | 1985-03-21 | Snam Progetti | PROCEDURE FOR THE PRODUCTION OF UREA AND PURIFICATION OF WATERS |
| UA26895C2 (en) * | 1990-03-12 | 1999-12-29 | Уріа Казале С.А. | Invention relates to the chemical technology of obtaining ammonia and carbon dioxide, method of improvement of operation and decrease of the effects of corrosion, at high temperatures and pressures, during condensation of ammonia, carbon dioxide and water vapors, which are obtained from the systems of so-called “stripping” of the solution in the reactor of obtaining urea. The method of condensation of vapors of ammonia, carbon dioxide and water that are formed during treatment of the solution, which is supplied from the reactor of obtaining urea, includes cooling vapors of ammonia, carbon dioxide and water in the urethane condenser equipped with the tube bundles of U-shaped form, with subsequent recirculation of a part of obtained solution of urethane and recuperation of the heat of condensation with formation of water vapor. |
| CN103349848B (en) * | 2013-06-18 | 2015-07-08 | 盐城汇百实业有限公司 | Condensing device |
| KR102564759B1 (en) | 2017-10-27 | 2023-08-07 | 스태미카본 비.브이. | High pressure carbamate condenser |
| AU2022420708A1 (en) | 2021-12-20 | 2024-07-04 | Stamicarbon B.V. | Thermal stripping urea production |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2302993A (en) * | 1940-12-07 | 1942-11-24 | Lummus Co | Evaporator |
| US2560070A (en) * | 1948-08-27 | 1951-07-10 | Lummus Co | Evaporator |
| CH498811A (en) * | 1967-05-22 | 1970-11-15 | Chemical Construction Corp | Process for the production of urea from ammonia and carbon dioxide |
| US3984469A (en) * | 1969-10-16 | 1976-10-05 | Snam Progetti S.P.A. | Process for the production of urea |
| US3940440A (en) * | 1970-11-10 | 1976-02-24 | Ivo Mavrovic | Method of controlling urea system |
-
1976
- 1976-04-20 US US05/678,635 patent/US4082797A/en not_active Expired - Lifetime
- 1976-04-20 GB GB16012/76A patent/GB1506129A/en not_active Expired
- 1976-04-20 DE DE2617185A patent/DE2617185C3/en not_active Expired
- 1976-04-22 NL NLAANVRAGE7604303,A patent/NL167157C/en not_active IP Right Cessation
- 1976-04-22 FR FR7611952A patent/FR2308615A1/en active Granted
- 1976-04-22 CS CS762673A patent/CS196306B2/en unknown
- 1976-04-23 JP JP51045614A patent/JPS6023109B2/en not_active Expired
- 1976-07-06 AU AU15623/76A patent/AU506832B2/en not_active Expired
- 1976-07-09 AT AT508576A patent/AT344197B/en not_active IP Right Cessation
- 1976-07-12 BE BE168843A patent/BE844047A/en not_active IP Right Cessation
- 1976-07-13 CH CH902776A patent/CH622006A5/en not_active IP Right Cessation
- 1976-07-17 IN IN1284/CAL/1976A patent/IN144536B/en unknown
- 1976-07-20 CA CA257,369A patent/CA1069932A/en not_active Expired
- 1976-07-21 SE SE7608335A patent/SE423386B/en not_active IP Right Cessation
Also Published As
| Publication number | Publication date |
|---|---|
| IN144536B (en) | 1978-05-13 |
| AU506832B2 (en) | 1980-01-24 |
| CA1069932A (en) | 1980-01-15 |
| FR2308615B1 (en) | 1979-04-20 |
| BE844047A (en) | 1977-01-12 |
| CH622006A5 (en) | 1981-03-13 |
| AU1562376A (en) | 1978-01-12 |
| NL167157C (en) | 1987-10-16 |
| DE2617185A1 (en) | 1976-10-28 |
| SE423386B (en) | 1982-05-03 |
| NL7604303A (en) | 1976-10-26 |
| FR2308615A1 (en) | 1976-11-19 |
| ATA508576A (en) | 1977-11-15 |
| GB1506129A (en) | 1978-04-05 |
| JPS51128917A (en) | 1976-11-10 |
| CS196306B2 (en) | 1980-03-31 |
| DE2617185B2 (en) | 1977-11-24 |
| SE7608335L (en) | 1978-01-22 |
| AT344197B (en) | 1978-07-10 |
| DE2617185C3 (en) | 1978-07-13 |
| US4082797A (en) | 1978-04-04 |
| NL167157B (en) | 1981-06-16 |
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